RU110289U1 - DEVICE FOR PRODUCING SYNTHESIS GAS - Google Patents

Abstract

 1. A device for producing axial type synthesis gas, comprising a mixing and distribution starting device, a heat exchanger and a catalytic reactor comprising one or more catalytic units, characterized in that the catalytic unit is made in the form of axial units of alternating flat and corrugated heat-conducting metal-porous catalytic tapes with the presence of channels for the passage of gas flows. ! 2. The device according to claim 1, characterized in that the corrugated heat-conducting metal-porous catalytic strip is made by the method of porous rolling of heat-conducting metal powders, followed by impregnation with a catalytically active mass. ! 3. The device according to claim 1, characterized in that the active components of the catalytically active mass are nickel, or magnesium, or any mixture thereof. ! 4. The device according to claim 1, characterized in that the heat exchanger can be integrated with a catalytic reactor. ! 5. The device according to claim 1, characterized in that it comprises a corridor type heat exchanger. ! 6. The device according to claim 1, characterized in that inside the mixing distribution distributor starting device is a starting system. ! 7. The device according to claim 6, characterized in that the starting system consists of a distribution cone with a tangential input and a spark plug or electric heating element.

Description

The invention relates to a device for the catalytic partial oxidation of gaseous hydrocarbon fuels and can be used to produce synthesis gas and its further use as additives to fuel in internal combustion engines and in power plants using fuel cells, as well as in heating water-heating systems for generating heat .

A device is known (RU 2175799, H01M 8/06, C01B 3/38, 11/10/2001), which can operate in the partial oxidation of hydrocarbon gas. The device involves the use of a package in which there are sequentially located inert "heat-conducting plates" and catalytic plates, while the isothermality of the process is ensured by the good (radial) thermal conductivity of only the "heat-conducting plate" to ensure an isothermal mode of hydrocarbon gas oxidation. It is known that partial oxidation proceeds through the methane oxidation stage and subsequent reforming reactions; therefore, because of the high exothermicity of the combustion reaction, “hot spots” arise in the first part of the fixed catalyst bed and therefore, the catalytic partial oxidation of methane is carried out in reactors at short contact times (fractions of seconds ) and thermal conductivity of the layer of at least 0.15 J / (sec m K) [M.Fafhi, RH Hofstad, T. Sperle, O.A. Rockstad, A. Holmen. Partial oxidation of methane to synthesis gas at very short contact times. // Catalysis Today 42, 1998, p.205-209]. The thickness of the catalytic layer provides a complete conversion of methane at a contact time of not more than 0.3 s. The temperature in the catalytic bed rises to 750-850 ° C. The most suitable material suitable for working under these conditions for a long time is an alloy of the composition Fe-Ni-Cr-Al or Fe-Cr-Al. Heat transfer from the surface of the catalytic layer to the external volume is carried out mainly by convection and infrared radiation; therefore, the occurrence of local “hot spots” on the catalytic plate is possible only by a significant increase in the thermal conductivity of the catalyst carrier, which allows the temperature to be redistributed over the cross section of the catalytic plate. The disadvantage of this design is that the isothermal process is provided by the installation of inert "heat-conducting plates." These plates are the ballast mass in the structure and when the heat conductivity of the material of these plates is less than 16 J / (sec m K), the plates must have a thickness several times greater than the thickness of the catalytic plates.

An integrated device for the reforming of hydrocarbons is known (US 6641625, B01J 8/04; C01B 3/36, 11/04/2003). The hydrocarbon reforming apparatus includes two reactors with a heat exchanger. The first reactor generates a hydrogen-containing gas through partial oxidation, steam reforming of hydrocarbon feedstock, or in another way. The second reactor contains a catalyst providing a shift reaction of a hydrogen-rich reformate. The heat exchanger provides the flow of steam necessary for carrying out the shift reaction into the second reactor.

Known catalytic reactor (RU 2208475, B01J 8/04; C01B 3/00, 07/20/2003) for producing radial-type synthesis gas containing a gas distribution pipe with a catalyst layer, which is made in the form of gas-permeable flat and corrugated reinforced tapes, wound and sintered with a gas distribution pipe with gaps between the turns with the formation of gas-air channels between the tapes. The reactor has a heating device to put it into operation. The gas distribution pipe has perforation holes with a diameter smaller than the critical diameter to prevent flame from entering the gas distribution pipe. As a catalyst, a reinforced porous material containing active components is used: rhodium, nickel, platinum, palladium, iron, cobalt, rhenium, ruthenium, or a mixture thereof.

The above device is the closest in technical essence to the claimed device and therefore is selected as a prototype.

The disadvantage of this device is the high complexity of manufacturing reinforced porous materials, a decrease in the total catalytic activity due to the use of reinforcing materials and the high temperature of the outgoing synthesis gas.

The invention solves the problem of creating a compact axial type device for producing synthesis gas from hydrocarbon gas with increased efficiency.

The problem is solved by the design of an apparatus for producing axial type synthesis gas, which contains a mixing and distribution starting device, a heat exchanger, a catalytic reactor, including one or more catalytic blocks, which are made in the form of axial blocks of alternating flat and corrugated heat-conducting metal-porous catalytic tapes with the presence of channels for the passage of gas flows.

Corrugated heat-conducting metal-porous catalytic tapes are made by the method of porous rolling of heat-conducting metal powders, followed by impregnation with a catalytically active mass.

Nickel or magnesium, or any mixture thereof, are used as active components of the catalytically active mass.

The heat exchanger can be integrated with a catalytic reactor. The device comprises a corridor type heat exchanger.

Inside the mixing and distributing starting device, a starting system is located, which consists of a distribution cone with a tangential input and a spark plug or electric heating element.

Chilled synthesis gas exits the device.

New is the implementation of the catalyst in the form of an axial block of alternating between a flat and corrugated heat-conducting metal-porous catalytic strip with the formation of channels for the passage of gas flows. The heat-conducting metal-porous catalytic strip is made by the method of porous rolling from heat-conducting metal powders, followed by impregnation with catalytically active elements.

New in this device is the manufacture of a catalytic unit from serial technologies of manufacturing metal-porous materials mastered by the industry, low labor intensity and cost, an increase in overall catalytic activity due to the use of porous nickel, which is catalytically active in the partial oxidation of hydrocarbon reactions, as a substrate. Inside the mixing distribution distribution starter is a launch system, which consists of a tangential input with a spark plug or an electric heating element. Also new is the on-board synthesis gas generator in the form of a compact integrated catalytic reactor and heat exchanger. The output time of the device to the operating mode is not more than 45 s.

Figure 1 presents the design of the claimed device.

Figure 2 presents the design of the mixing distribution starter.

The device comprises a sealed cylindrical cooled case with a mixing and distribution starting device 1, a tangential inlet 2, a spark plug 3 or an electric heating element, a catalytic reactor comprising one or more catalytic units, 4 and an integrated corridor-type heat exchanger 5. Catalytic unit (or blocks) is made in the form of an axial block of alternating flat and corrugated heat-conducting metal-porous catalytic tapes. Corrugated heat-conducting metal-porous catalytic strip is made by the method of porous rolling of heat-conducting metal powders, followed by impregnation with a catalytically active mass. In the block, triangular grooves are made from the center to the periphery, providing axial passage of the reaction mixture. The grooves in the catalytic unit are in the shape of a triangle. A package of catalytic units to ensure thermal (thermal) contact is pulled together between two rigid supporting devices using studs. Metal-porous heat-conducting catalytic tapes are made by the method of porous rolling, porosity of 40-50%, followed by impregnation with a catalytically active mass. As a catalyst, active components containing nickel or magnesium, or mixtures thereof are used.

The annular gap formed by the inner surface of the housing and the outer cylindrical surface of the catalytic package forms a collector for the removal of synthesis gas into the heat exchanger. The uniform distribution of the reformed mixture over the cross section of the catalytic unit is ensured by the mixing and distributing starting device 1. Inside the mixing and distributing starting device, there is a gas starting system, which consists of a spark plug (spark or glow) or an electric heating element (TENA). The mixing and distribution device is made in the form of a cone, and the flow of hydrocarbon gas and air is twisted relative to the axis of the cone with the help of a tangential input, which ensures the homogeneity of the hydrocarbon gas-air mixture, both at the stage of partial oxidation and at start-up (heating) - in the full mode oxidation. The reactor is launched by heating the catalytic unit to the temperature of the onset of the partial oxidation reaction. The heating of the catalytic unit is carried out by heating the hydrocarbon gas oxidation products, while the ignition of the hydrocarbon gas-air mixture is produced by a spark plug (spark or incandescent).

The design of the proposed catalytic reactor through the use of metalloporous heat-conducting catalytic carrier having good thermal conductivity, provides a mode close to isothermal. The nominal capacity of the onboard synthesis gas generator can be changed by changing the diameter and length of the catalytic unit. The dimensions of the catalytic unit are determined by the required performance, activity of the catalyst. The recommended thickness of the catalytic ribbon is 90 microns, the width of the catalytic ribbon is 54 mm, the corrugation height of the catalytic ribbon is 1.2-2 mm.

The device operates as follows.

Initial reagents: hydrocarbon gas and air in the ratio α = 0.85-1 are fed through the tangential input 2 to the mixing and distributing starting device 1. In the mixing and distributing starting device 1, the gases are mixed to a uniform state and then the mixed stream enters the zone of the candle 3. The mixture lights up and the combustion products (flue gases) warm up the catalytic unit. When the catalytic unit is heated to the temperature of the onset of partial oxidation (500-600 ° C), the ratio of hydrocarbon gas to air changes to α≈0.25-0.3. This mixture, passing through the catalytic unit, undergoes partial oxidation with the release of synthesis gas containing up to 33% hydrogen and up to 16-17% carbon monoxide when using natural gas as a hydrocarbon gas. Next, the hot synthesis gas enters the integrated heat exchanger, where with the help of antifreeze, the temperature of the synthesis gas is reduced from 750 C to 150 C.

The proposed device allows you to convert part of the fuel into synthesis gas on board the vehicle. The addition of synthesis gas to the main fuel makes it possible to reduce fuel consumption by 20-25% during idle conditions and to achieve Euro-4 standards without installing a catalytic converter. It also allows to reduce operating fuel consumption and to provide a significant reduction in toxic emissions in the exhaust gases of an engine, including CO ₂ , which creates a greenhouse effect.

Claims (7)

1. A device for producing axial type synthesis gas, comprising a mixing and distribution starting device, a heat exchanger and a catalytic reactor comprising one or more catalytic units, characterized in that the catalytic unit is made in the form of axial units of alternating flat and corrugated heat-conducting metal-porous catalytic tapes with the presence of channels for the passage of gas flows. 2. The device according to claim 1, characterized in that the corrugated heat-conducting metal-porous catalytic strip is made by the method of porous rolling of heat-conducting metal powders, followed by impregnation with a catalytically active mass. 3. The device according to claim 1, characterized in that the active components of the catalytically active mass are nickel, or magnesium, or any mixture thereof. 4. The device according to claim 1, characterized in that the heat exchanger can be integrated with a catalytic reactor. 5. The device according to claim 1, characterized in that it comprises a corridor type heat exchanger. 6. The device according to claim 1, characterized in that inside the mixing distribution distributor starting device is a starting system. 7. The device according to claim 6, characterized in that the starting system consists of a distribution cone with a tangential input and a spark plug or electric heating element.